JP2001233831A - Method for producing ethylene carbonate - Google Patents
Method for producing ethylene carbonateInfo
- Publication number
- JP2001233831A JP2001233831A JP2000042349A JP2000042349A JP2001233831A JP 2001233831 A JP2001233831 A JP 2001233831A JP 2000042349 A JP2000042349 A JP 2000042349A JP 2000042349 A JP2000042349 A JP 2000042349A JP 2001233831 A JP2001233831 A JP 2001233831A
- Authority
- JP
- Japan
- Prior art keywords
- reaction
- ethylene oxide
- reaction solution
- reactor
- liquid
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
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Classifications
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/141—Feedstock
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明はエチレンオキシドと
二酸化炭素とを反応させてエチレンカーボネートを製造
する方法に関するものである。特に本発明は純度のよい
エチレンカーボネートを高収率で、かつ効率よく製造す
る方法に関するものである。TECHNICAL FIELD The present invention relates to a method for producing ethylene carbonate by reacting ethylene oxide with carbon dioxide. In particular, the present invention relates to a method for efficiently producing high-purity ethylene carbonate in high yield.
【０００２】[0002]
【従来の技術】エチレンカーボネートは、リチウムイオ
ン電池の電解液として需要が伸びているほか、ポリカー
ボネートの炭酸基の原料としても有望視されている。エ
チレンカーボネートの工業的製造法としては、エチレン
オキシドと二酸化炭素を反応させる方法が最も一般的で
ある。2. Description of the Related Art Ethylene carbonate is expected to be used as an electrolyte for lithium ion batteries and also as a raw material for carbonate groups of polycarbonate. The most common industrial production method of ethylene carbonate is a method of reacting ethylene oxide with carbon dioxide.
【０００３】[0003]
【発明が解決しようとする課題】エチレンオキシドと二
酸化炭素からのエチレンカーボネートの生成反応は液相
で進行するので、大きな反応速度で反応を行わせるに
は、液相への二酸化炭素の溶解を促進することが必要で
ある。また、この反応は非常に大きな発熱を伴い、暴走
反応を起こし易い。暴走反応は、触媒の分解やアルデヒ
ドなどの副生物の生成を増大させ、エチレンカーボネー
トの品質に著しい悪影響を与えるので、是非とも回避し
なければならない。Since the reaction for producing ethylene carbonate from ethylene oxide and carbon dioxide proceeds in a liquid phase, the dissolution of carbon dioxide in the liquid phase is promoted in order to carry out the reaction at a high reaction rate. It is necessary. In addition, this reaction is accompanied by a very large amount of heat and easily causes a runaway reaction. Runaway reactions must be avoided because they increase the decomposition of the catalyst and the formation of by-products such as aldehydes, and have a significant adverse effect on the quality of ethylene carbonate.
【０００４】エチレンオキシドと二酸化炭素からエチレ
ンカーボネートを製造する反応装置としては、複数の管
型反応器と冷却器を直列に配置したもの（Ｓｐｒｉｎｇ
ｍａｎｎ，“Ｆｅｔｔｅ ｓｅｉｆｅｎ ａｎｓｔｒｉ
ｃｈｅｍｉｔｔｅｌ”，ｖｏｌ．７３，ｐ３９６〜３９
９（１９７１））、ループ型反応器（Ｐｅｐｐｅｌ，Ｉ
ｎｄｕｓｔｒｉａｌ ａｎｄ Ｅｎｇｉｎｅｅｒｉｎ
ｇ，Ｖｏｌ．５０，ｐ７６７〜７７０（１９５８））、
気泡塔（特開平６−３４５６９９号公報）など、さまざ
まなものが提案されているが、いずれも問題が多い。As a reactor for producing ethylene carbonate from ethylene oxide and carbon dioxide, a reactor in which a plurality of tubular reactors and a cooler are arranged in series (Spring)
mann, "Fette seifen anstri
chemittel ", vol. 73, pp. 396-39.
9 (1971)), loop reactor (Peppel, I
ndustrial and Engineerine
g, Vol. 50, pp. 767-770 (1958)),
Various types such as a bubble column (JP-A-6-345699) have been proposed, but all have many problems.
【０００５】先ず一般に用いられることの多い多管型反
応器では、各反応管に均一に二酸化炭素を供給するのが
困難である。また管内で二酸化炭素が反応液中に均一に
分散せずに気相部と液相部が分離し易い。その結果、反
応成績が安定せず、かつ除熱が良好に行われないので暴
走反応が起きる危険性がある。攪拌機を有する槽型の反
応器では、多大の攪拌動力を消費しても二酸化炭素を十
分に溶解させることは困難である。また、反応器の上部
の攪拌軸の摺動部からのガスの漏洩や、摺動部での摩擦
熱によりエチレンオキシドが爆発する可能性があり、有
毒で爆発性のエチレンオキシドを取扱うには安全性の点
でも問題がある。First, it is difficult to uniformly supply carbon dioxide to each reaction tube in a multi-tube reactor which is generally used. Further, the carbon dioxide is not uniformly dispersed in the reaction liquid in the tube, and the gas phase and the liquid phase are easily separated. As a result, the reaction results are not stable, and the heat removal is not performed well, and there is a risk that a runaway reaction occurs. In a tank reactor having a stirrer, it is difficult to sufficiently dissolve carbon dioxide even if a large amount of stirring power is consumed. In addition, there is a possibility that ethylene oxide may explode due to leakage of gas from the sliding part of the stirring shaft at the top of the reactor and frictional heat at the sliding part, and it is safe to handle toxic and explosive ethylene oxide. There is also a problem in point.
【０００６】気泡塔はこれらの反応装置に比較すると優
れているが、二酸化炭素の溶解を促進し、かつ塔内温度
を均一にするには、エチレンオキシドに対して過剰量の
二酸化炭素を存在させ、かつ二酸化炭素を循環させて反
応液を攪拌する必要がある。エチレンオキシドと二酸化
炭素からのエチレンカーボネートの生成反応は、水を添
加すると飛躍的に加速される。しかし水の添加はエチレ
ングリコールを副生させるので、水を添加せずに反応を
促進する方法が求められている。また反応を高温で行っ
ても反応は促進されるが、高温での反応は同時にアルデ
ヒドの生成などの副反応の増大を招くので、生成するエ
チレンオキシドの品質を悪化させる。従って本発明は、
水を添加せずとも、また高温で反応させずとも、十分に
大きな反応速度で反応を行うことのできる方法を提供し
ようとするものである。[0006] The bubble column is superior to these reactors, but in order to promote the dissolution of carbon dioxide and to make the temperature in the column uniform, an excess amount of carbon dioxide with respect to ethylene oxide must be present. Further, it is necessary to stir the reaction solution by circulating carbon dioxide. The reaction for producing ethylene carbonate from ethylene oxide and carbon dioxide is dramatically accelerated by adding water. However, since the addition of water produces ethylene glycol as a by-product, there is a need for a method of accelerating the reaction without adding water. Although the reaction is accelerated even when the reaction is carried out at a high temperature, the reaction at a high temperature causes an increase in side reactions such as the formation of an aldehyde at the same time, thereby deteriorating the quality of the produced ethylene oxide. Therefore, the present invention
An object of the present invention is to provide a method capable of performing a reaction at a sufficiently high reaction rate without adding water or performing a reaction at a high temperature.
【０００７】[0007]
【課題を解決するための手段】本発明によれば、エチレ
ンオキシドと二酸化炭素とを、カーボネート化触媒の存
在下に反応させてエチレンカーボネートを製造するに際
し、反応液滞留部とその上方に気相部を有し、かつ気相
部にエジエクターが設置されている反応器を用いて、
（イ）反応液滞留部の下部から反応液を抜出しこれを循
環導管を介して気相部に設置されているエジエクターに
送り、エジエクターにおいて気相部のガスを吸引してか
ら気相部に噴射すること、（ロ）エジエクターから単位
時間当り噴射される反応液の量は、単位時間に供給され
るエチレンオキシドの１０重量倍以上であること、
（ハ）反応液滞留部の液表面の直径に対する表面から反
応液抜出口までの液深の比が２倍以上であることの各条
件を満足するように反応を行わせることにより、大きな
反応速度で不純物の少ないエチレンカーボネートを製造
することができる。According to the present invention, in producing ethylene carbonate by reacting ethylene oxide and carbon dioxide in the presence of a carbonate catalyst, a reaction solution stagnation portion and a gas phase portion above the reaction solution stagnation portion are provided. Using a reactor having an ejector in the gas phase,
(A) Withdrawing the reaction solution from the lower part of the reaction solution storage section, sending the reaction solution to an ejector installed in the gas phase via a circulation conduit, sucking the gas in the gas phase in the ejector, and injecting the gas into the gas phase (B) the amount of the reaction solution injected per unit time from the ejector is at least 10 times the weight of ethylene oxide supplied per unit time;
(C) A large reaction rate is obtained by performing the reaction so as to satisfy each condition that the ratio of the liquid depth from the surface to the outlet of the reaction liquid to the diameter of the liquid surface in the reaction liquid retaining section is twice or more. Thus, ethylene carbonate with less impurities can be produced.
【０００８】このようなエジエクターを有する反応装置
は、本発明者によるエチレングリコールの製造（特願平
１０−６９９８３号）や、Ｂｕｓｓ社によるエトキシレ
ートの製造（特開平３−１４８２３４号公報）などでも
用いられているが、上記のような条件で反応を行うこと
は記載されていない。本発明者は上記の条件で反応を行
えば、反応液中に二酸化炭素を微細な気泡として分散さ
せることができ、その結果、反応が円滑に進行し、不純
物の少ないエチレンカーボネートが生成することを見出
したものである。[0008] The reaction apparatus having such an ejector is also used for the production of ethylene glycol by the present inventor (Japanese Patent Application No. 10-69983) and the production of ethoxylate by Buss (Japanese Patent Application Laid-Open No. 3-148234). Although it is used, it is not described that the reaction is carried out under the above conditions. The present inventor can conduct the reaction under the above conditions to disperse carbon dioxide as fine bubbles in the reaction solution, and as a result, the reaction proceeds smoothly, and ethylene carbonate with less impurities is produced. It was found.
【０００９】[0009]
【発明の実施の形態】本発明では反応液滞留部とその上
部に気相部を有している反応器を用いる。反応器の気相
部には反応液を駆動流体とするエジエクターが設置され
ており、エジエクターと反応液滞留部の下部とは、途中
に循環ポンプを有する循環導管で連絡されている。従っ
て反応液は反応液滞留部の下部から循環導管に抜出さ
れ、ポンプで加圧されてエジエクターに送られ、エジエ
クターから気相部に噴射される。このときエジエクター
の吸引部で気相部のガスを吸引させる。これにより気相
部のガスの主体をなす二酸化炭素が、エジエクターを通
過する反応液中に微細な気泡となって分散・溶解する。BEST MODE FOR CARRYING OUT THE INVENTION In the present invention, a reactor having a reaction solution retaining section and a gas phase section above the same is used. An ejector using a reaction liquid as a driving fluid is installed in a gas phase part of the reactor, and the ejector is connected to a lower part of the reaction liquid retention part by a circulation pipe having a circulation pump in the middle. Therefore, the reaction solution is withdrawn from the lower part of the reaction solution holding section into the circulation conduit, pressurized by a pump, sent to the ejector, and injected from the ejector into the gas phase section. At this time, the gas in the gas phase is sucked by the suction unit of the ejector. As a result, carbon dioxide, which is the main component of the gas in the gas phase, is dispersed and dissolved as fine bubbles in the reaction liquid passing through the ejector.
【００１０】本発明では単位時間当り、供給されるエチ
レンオキシドの１０重量倍以上の反応液をエジエクター
に供給する。これにより反応液には常に反応を促進する
に十分な量の二酸化炭素を存在させることができ、大き
な反応速度でエチレンカーボネートの生成反応を行わせ
ることができる。反応器は、気相部に噴射された反応液
が反応液滞留部の液抜出口に到達するまでに、エジエク
ターで反応液中に小気泡となって分散したガスが反応液
に溶解するか又は反応液から分離して抜け出すように、
その反応液滞留部は細長い形状であるべきである。気泡
を含む反応液が循環導管に吸引されると、循環ポンプが
キャビテーションを起すおそれがある。本発明では、反
応液滞留部の液表面から循環導管への液抜出口までの距
離、すなわち液深が、液表面の直径（ここに直径とは、
液表面の面積と等しい面積の円の直径を意味する）の２
倍以上となるように反応器内に反応液を存在させる。な
お、液深に対する直径の比が２以上の反応器を用いて
も、循環液量が多過ぎると、気泡を含む反応液が循環導
管に抜き出されるおそれがあるので注意を要する。In the present invention, a reaction solution is supplied to an ejector at a rate of 10 times or more of the supplied ethylene oxide per unit time. As a result, a sufficient amount of carbon dioxide can be always present in the reaction solution to promote the reaction, and the formation reaction of ethylene carbonate can be performed at a high reaction rate. By the time the reaction liquid injected into the gas phase part reaches the liquid outlet of the reaction liquid retention part, the gas dispersed as small bubbles in the reaction liquid by the ejector is dissolved in the reaction liquid or So that it separates from the reaction solution and escapes
The reaction solution reservoir should have an elongated shape. When the reaction solution containing bubbles is sucked into the circulation conduit, the circulation pump may cause cavitation. In the present invention, the distance from the liquid surface of the reaction liquid retaining section to the liquid outlet to the circulation conduit, that is, the liquid depth is the diameter of the liquid surface (here, the diameter is
(Meaning the diameter of a circle having an area equal to the area of the liquid surface)
The reaction solution is present in the reactor so as to be at least twice as large. It should be noted that even if a reactor having a ratio of the diameter to the liquid depth of 2 or more is used, if the amount of the circulating liquid is too large, the reaction liquid containing bubbles may be drawn out to the circulation conduit.
【００１１】本発明においては、エチレンカーボネート
の生成反応そのものは常法に従って行われる。カーボネ
ート化反応の触媒としては、アルカリ金属の臭化物又は
ヨウ化物（特公昭３８−２３１７５号公報）、アルカリ
土類金属のハロゲン化物（米国特許第２，６６７，４９
７号明細書）、アルキルアミン、第４級アンモニウム塩
（米国特許第２，７７３，０７０号明細書）、有機スズ
又はゲルマニウム若しくはテルル化合物（特開昭５７−
１８３７８４号公報）、ハロゲン化有機ホスホニウム塩
（特開昭５８−１２６８８４号公報）など公知のものを
用いればよい。活性や選択性の点からは、臭化カリウム
やヨウ化カリウム等のアルカリ金属ハロゲン化物、ハロ
ゲン化有機ホスホニウム塩などを用いるのが好ましい。
触媒の供給量は触媒の種類や反応条件により異なるが、
例えばトリブチルメチルホスホニウムアイオダイドであ
れば、エチレンオキシドに対して０．００１〜０．０５
モル倍となるように用いるのが好ましい。反応系に供給
するエチレンオキシドと二酸化炭素の比率は反応条件に
より定まる。すなわち反応系に供給された二酸化炭素
は、一部はエチレンカーボネートの生成に消費され、残
部は反応液に同伴して系外に抜出されるが、その同伴量
は温度や圧力などの反応条件により定まるからである。
エチレンオキシドの反応率を高めるため二酸化炭素を過
剰、通常はモル比で３倍程度まで、に供給するのが好ま
しい。エチレンオキシド及び二酸化炭素の供給位置は任
意である。例えば二酸化炭素をエジエクターの吸引部に
供給するのも好ましい。In the present invention, the ethylene carbonate formation reaction itself is carried out according to a conventional method. As catalysts for the carbonate reaction, bromides or iodides of alkali metals (Japanese Patent Publication No. 38-23175) and halides of alkaline earth metals (US Pat. No. 2,667,49)
No. 7), alkylamines, quaternary ammonium salts (U.S. Pat. No. 2,773,070), organotins or germanium or tellurium compounds (Japanese Patent Application Laid-Open No. 57-070).
183784) and known organic phosphonium salts (Japanese Patent Laid-Open No. 58-126884). From the viewpoint of activity and selectivity, it is preferable to use an alkali metal halide such as potassium bromide or potassium iodide, or an organic phosphonium halide salt.
The amount of catalyst supply varies depending on the type of catalyst and reaction conditions,
For example, in the case of tributylmethylphosphonium iodide, 0.001-0.05 to ethylene oxide
It is preferable to use it in a molar ratio. The ratio of ethylene oxide and carbon dioxide supplied to the reaction system is determined by the reaction conditions. That is, part of the carbon dioxide supplied to the reaction system is consumed for the production of ethylene carbonate, and the remainder is extracted out of the system along with the reaction solution, but the amount of entrainment depends on reaction conditions such as temperature and pressure. Because it is decided.
In order to increase the reaction rate of ethylene oxide, it is preferable to supply carbon dioxide in excess, usually up to about 3 times in molar ratio. The supply positions of ethylene oxide and carbon dioxide are arbitrary. For example, it is also preferable to supply carbon dioxide to the suction unit of the ejector.
【００１２】反応温度は通常７０〜２００℃であるが、
反応を円滑に進行させ、かつ副反応を抑制するには１０
０〜１８０℃で反応させるのが好ましい。また反応圧力
は通常５〜５０ｋｇ／ｃｍ2 Ｇであるが１０〜３０ｋｇ
／ｃｍ2 Ｇが好ましい。反応圧力が高いほど二酸化炭素
の溶解が促進されるが、圧縮器及び循環ポンプの動力費
が増加する。エチレンオキシドと二酸化炭素からのエチ
レンカーボネートの生成反応は大きな発熱を伴うので、
反応熱の除去が必要である。反応熱の除去は反応器の反
応液滞留部に除熱用コイルを設置することにより行うこ
ともできるが、循環導管の途中に多管式熱交換器を設置
するのが好ましい。The reaction temperature is usually from 70 to 200 ° C.,
To make the reaction proceed smoothly and suppress side reactions, 10
The reaction is preferably performed at 0 to 180 ° C. The reaction pressure is usually 5 to 50 kg / cm 2 G, but 10 to 30 kg.
/ Cm 2 G is preferred. Higher reaction pressures promote carbon dioxide dissolution, but increase the power costs of the compressor and circulation pump. Since the reaction to produce ethylene carbonate from ethylene oxide and carbon dioxide involves a large amount of heat,
Removal of heat of reaction is required. The reaction heat can be removed by installing a heat removal coil in the reaction solution retaining portion of the reactor, but it is preferable to install a multi-tube heat exchanger in the middle of the circulation conduit.
【００１３】本発明によれば反応液は反応器内で激しく
撹拌されて全体がほぼ均一となっているので、連続方式
で反応させる場合にはこの反応系で反応を完結させるの
は困難であり、反応液には常に未反応のエチレンオキシ
ドが含まれている。従って反応器から抜出した反応液
は、ピストンフロー方式の管式反応器に導入して更に反
応させ、エチレンオキシドの反応率を向上させるのが好
ましい。この場合、管式反応器に導入される反応液に
は、エチレンオキシドに対して過剰の二酸化炭素を存在
させ、もってエチレンオキシドの反応を促進するのが好
ましい。通常は反応液中のエチレンオキシドの濃度が１
重量％以下、好ましくは０．１〜０．５重量％となるま
で反応器で反応させ、この反応液を管式反応器に導入し
て更に反応させるのが好ましい。管式反応器では反応液
中のエチレンオキシドが１０重量部ｐｐｍ以下、すなわ
ちエチレンオキシドが実質上存在しなくなるまで反応さ
せるのが好ましい。According to the present invention, since the reaction solution is vigorously stirred in the reactor and the whole is almost uniform, it is difficult to complete the reaction in this reaction system when the reaction is carried out in a continuous system. The reaction solution always contains unreacted ethylene oxide. Therefore, it is preferable that the reaction liquid drawn out of the reactor is introduced into a tubular reactor of a piston flow type to further react to improve the reaction rate of ethylene oxide. In this case, it is preferable that the reaction liquid introduced into the tubular reactor contains excess carbon dioxide with respect to ethylene oxide, thereby promoting the reaction of ethylene oxide. Usually, the concentration of ethylene oxide in the reaction solution is 1
It is preferable to carry out the reaction in the reactor until the amount becomes not more than 0.1% by weight, preferably 0.1 to 0.5% by weight, and to introduce the reaction solution into a tubular reactor for further reaction. In a tubular reactor, the reaction is preferably performed until the ethylene oxide in the reaction solution is 10 parts by weight or less, that is, until ethylene oxide is substantially absent.
【００１４】[0014]
【実施例】以下に実施例により本発明を更に具体的に説
明するが、本発明は以下の実施例に限定されるものでは
ない。 実施例１ 内径３０ｃｍ、塔高１００ｃｍの円筒状反応器を用いて
エチレンオキシドと二酸化炭素とを反応させてエチレン
カーボネートを製造した。反応器の頂部にはエジエクタ
ーが設置されており、反応器の底部とエジエクターと
は、途中に熱交換器及び循環ポンプを介して循環導管で
連絡されている。この循環導管の途中には、循環導管と
管式反応器（直径５ｃｍ、長さ５ｍ）とを連結する反応
液抜出管が取付けられている。管式反応器は断熱状態で
反応が進行するように断熱材で被覆されている。EXAMPLES The present invention will be described more specifically with reference to the following examples, but the present invention is not limited to the following examples. Example 1 Ethylene oxide was produced by reacting ethylene oxide and carbon dioxide using a cylindrical reactor having an inner diameter of 30 cm and a tower height of 100 cm. An ejector is provided at the top of the reactor, and the bottom of the reactor and the ejector are connected on the way with a circulation conduit via a heat exchanger and a circulation pump. In the middle of the circulation conduit, a reaction liquid discharge pipe connecting the circulation conduit and a tubular reactor (diameter 5 cm, length 5 m) is attached. The tubular reactor is covered with a heat insulating material so that the reaction proceeds in an adiabatic state.
【００１５】エチレンカーボネート１５．４ｋｇ／Ｈｒ
に、エチレンオキシド１１．０ｋｇ／Ｈｒとヨウ化カリ
ウム２．０ｋｇ／Ｈｒを溶解させてエジエクターの手前
で循環導管に連続的に供給した。二酸化炭素は、反応器
の気相部の圧力が２０ｋｇ／ｃｍ2 Ｇとなるように気相
部に供給した。反応液は２７０ｋｇ／Ｈｒで循環導管を
経てエジエクターに送り、エジエクターで気相部のガス
を吸引させてから気相部に噴射した。反応器内の温度は
１８０℃に制御した。反応液は反応器内の液深が９０ｃ
ｍとなるように連続的に抜出して管式反応器に導入し
た。このようにして連続的に反応を行わせた結果、定常
状態において管式反応器に導入される反応液のエチレン
オキシドの濃度は０．１０重量％であり、炭酸ガスの濃
度は１．１重量％であった。反応器でのエチレンオキシ
ド基準のエチレンカーボネートの収率は９９％以上であ
った。また管式反応器出口の反応液の温度は１８２℃で
あり、その中のエチレンオキシド濃度は検出限界である
１０重量ｐｐｍ以下であった。15.4 kg / hr of ethylene carbonate
And 11.0 kg / Hr of ethylene oxide and 2.0 kg / Hr of potassium iodide were dissolved therein and continuously supplied to a circulation conduit before an ejector. Carbon dioxide was supplied to the gas phase so that the pressure in the gas phase of the reactor became 20 kg / cm 2 G. The reaction solution was sent to the ejector via a circulation conduit at 270 kg / Hr, and the gas in the gas phase was sucked by the ejector and then injected into the gas phase. The temperature inside the reactor was controlled at 180 ° C. The reaction liquid has a liquid depth of 90 c in the reactor.
m and continuously introduced into a tubular reactor. As a result of the continuous reaction as described above, in the steady state, the concentration of ethylene oxide in the reaction solution introduced into the tubular reactor was 0.10% by weight, and the concentration of carbon dioxide gas was 1.1% by weight. Met. The yield of ethylene carbonate based on ethylene oxide in the reactor was 99% or more. The temperature of the reaction solution at the outlet of the tubular reactor was 182 ° C., and the ethylene oxide concentration therein was 10 ppm by weight or less, which is the detection limit.
Claims (3)
ーボネート化触媒の存在下に反応させて、エチレンカー
ボネートを製造するに際し、反応液滞留部とその上方に
気相部を有し、かつ気相部にエジエクターが設置されて
いる反応器を用いて、 （イ）反応液滞留部の下部から反応液を抜出し、これを
循環導管を介して気相部に設置されているエジエクター
に送り、エジエクターにおいて気相部のガスを吸引して
気相部に噴射すること、 （ロ）エジエクターから単位時間当り噴射される反応液
の量は、単位時間当り供給されるエチレンオキシドの１
０重量倍以上であること、 （ハ）反応液滞留部の液表面の直径に対する反応液抜出
口までの液深の比が２倍以上であることの各条件を満足
するように反応を行うことを特徴とする方法。When producing ethylene carbonate by reacting ethylene oxide and carbon dioxide in the presence of a carbonation catalyst, a reaction solution stagnation portion and a gas phase portion above the reaction solution retention portion are provided. Using a reactor equipped with an ejector, (a) Withdrawing the reaction solution from the lower part of the reaction solution retaining section, sending the reaction solution through a circulation conduit to an ejector installed in the gas phase section, and (B) The amount of the reaction liquid injected per unit time from the ejector is one of the ethylene oxide supplied per unit time.
(C) The reaction should be performed so as to satisfy the conditions that the ratio of the liquid depth to the outlet of the reaction liquid to the diameter of the liquid surface of the reaction liquid retaining part is twice or more. A method characterized by the following.
ｃｍ2 Ｇで行うことを特徴とする請求項１記載の方法。2. The reaction is carried out at 70 to 200 ° C. and 5 to 50 kg /
The method according to claim 1, characterized in that in cm 2 G.
度が１重量％以下となるように反応を行い、かつ反応器
から抜出した反応液を管式反応器に供給してエチレンオ
キシドの濃度が１０重量ｐｐｍ以下となるまで反応させ
ることを特徴とする請求項１又は２記載の方法。3. The reaction is carried out so that the ethylene oxide concentration of the reaction solution in the reactor is 1% by weight or less, and the reaction solution discharged from the reactor is supplied to a tubular reactor to reduce the ethylene oxide concentration to 10% by weight. 3. The method according to claim 1, wherein the reaction is carried out until the amount becomes less than ppm.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2000042349A JP4019592B2 (en) | 2000-02-21 | 2000-02-21 | Method for producing ethylene carbonate |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2000042349A JP4019592B2 (en) | 2000-02-21 | 2000-02-21 | Method for producing ethylene carbonate |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JP2001233831A true JP2001233831A (en) | 2001-08-28 |
| JP4019592B2 JP4019592B2 (en) | 2007-12-12 |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2006104093A (en) * | 2004-10-01 | 2006-04-20 | Asahi Kasei Chemicals Corp | Manufacturing method of alkylene carbonate |
| KR100668043B1 (en) * | 2005-06-14 | 2007-01-15 | 한국과학기술연구원 | Production method of ethylene carbonate using loop reactor |
| US8329959B2 (en) | 2007-12-06 | 2012-12-11 | Shell Oil Company | Process for the preparation of alkylene glycol |
| JP2016190799A (en) * | 2015-03-31 | 2016-11-10 | 大日精化工業株式会社 | Method for producing 5-membered ring cyclic carbonate compounds |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH11269110A (en) * | 1998-03-19 | 1999-10-05 | Mitsubishi Chemical Corp | Production of monoethylene glycol |
-
2000
- 2000-02-21 JP JP2000042349A patent/JP4019592B2/en not_active Expired - Fee Related
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH11269110A (en) * | 1998-03-19 | 1999-10-05 | Mitsubishi Chemical Corp | Production of monoethylene glycol |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2006104093A (en) * | 2004-10-01 | 2006-04-20 | Asahi Kasei Chemicals Corp | Manufacturing method of alkylene carbonate |
| JP4624055B2 (en) * | 2004-10-01 | 2011-02-02 | 旭化成ケミカルズ株式会社 | Method for producing alkylene carbonate |
| KR100668043B1 (en) * | 2005-06-14 | 2007-01-15 | 한국과학기술연구원 | Production method of ethylene carbonate using loop reactor |
| US8329959B2 (en) | 2007-12-06 | 2012-12-11 | Shell Oil Company | Process for the preparation of alkylene glycol |
| US8530706B2 (en) | 2007-12-06 | 2013-09-10 | Shell Oil Company | Process for the preparation of alkylene glycol |
| JP2016190799A (en) * | 2015-03-31 | 2016-11-10 | 大日精化工業株式会社 | Method for producing 5-membered ring cyclic carbonate compounds |
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| Publication number | Publication date |
|---|---|
| JP4019592B2 (en) | 2007-12-12 |
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